Process and apparatus for removing methane or another fluid from a fluid mixture

ABSTRACT

A method and apparatus for separating a first fluid from a fluid mixture. In one embodiment water containing methane is passed through an agitation chamber with a plate at the chamber&#39;s proximal and distal ends. Both plates have orifices permitting the mixed fluid to pass into and out of the agitation chamber. In one embodiment, the mixed fluid rotates about its axis of flow through the agitation chamber. In one embodiment, the mixed fluid passes through a separation chamber having a plurality of baffles that promote separation of the methane from the methane/water mixture. In one embodiment, the separated methane is removed from the water in a collection chamber that facilitates gravity separation of the mixed fluids.

BACKGROUND OF THE INVENTION

A fluid may comprise a mixture of fluids with different properties. Forexample, some fluids are liquids containing entrained gas, other fluidsmay combine liquids having different physical properties such as oil andwater mixtures. Water removed from coal seams often contains entrainedmethane and other gases. Methane may partially separate from coal seamwater during pumping. However, this partial separation may beinefficient in that entrained methane often remains in the water pumpedfrom the seam. The entrained methane is a valuable commodity in and ofitself. As is well known, methane is an efficient and environmentallyfriendly fuel, producing water and carbon dioxide when burned.

Methane left in water can create numerous problems. Water-laden methanerequires additional chlorine demand in water disinfection systems. Theincreased use of chlorine in water treatment increases EPA-regulatedby-products. Additionally, the colorless and odorless methane can be anexplosion and fire hazard in water supplies. Pumping methane water canalso be difficult because the methane can create gas locks.

Entrained methane can be removed from water by letting the water restfor an extended period of time. Such is often accomplished in anenclosed tank, with valves and/or piping that vent the methane evolvedto the atmosphere or by placing the water in an open pond, as occurs inthe coal bed methane fields in the Powder River Basin of Wyoming. Attimes the removal is enhanced by air sparging (adding air to the water)or by adding chemicals to the methane/water mixture. Because methane isodorless and colorless, it escapes unnoticed into the atmosphere.

Methane is known as a particularly damaging greenhouse gas. Methanetakes years to breakdown naturally in the atmosphere. When itdecomposes, it creates carbon dioxide, a greenhouse gas. Methane is over20 times more effective at trapping heat in the atmosphere than carbondioxide.

The amount of methane escaping into the atmosphere is significant. It isbelieved Powder River Basin coal bed methane wells are between 75% and98% efficient in separating methane gas from pumped coal bed water. Ifexisting Powder River Basin coal bed methane wells average 85%efficiency, 675,000 mcf of methane escapes into the atmosphere from justPowder River Basin wells each day.

Coal bed water is not the only fluid containing potentially harmfulfluids. Entrained gases and volatile compounds may be found in pollutedgroundwater. For example, radon is a harmful gas that may be found inground water. Additionally, hydrocarbon gases other than methane mayalso be found in ground water. It is undesirable to vent the entrainedgases or compounds in polluted groundwater to the atmosphere becausethey may be toxic and may also contribute to greenhouse gas pollution.

Additionally, it may be desirable to separate mixtures of fluids havingdifferent physical properties. For example, crude oil spilled orreleased into water can cause significant environmental damage. Theoil/water mixture may also contain gases. Also, motor oil, or otherliquids, may be spilled or released into groundwater. Methods exist forremoving such fluids from water but the known methods requiresignificant energy input, are relatively inefficient and slow and mayintroduce harmful greenhouse gases into the atmosphere.

Currently used methods and apparatus for removing unwanted fluids fromfluid mixtures are slow and relatively inefficient and often releaseunwanted greenhouse gases. Heretofore, efficient and cost effectivemethods and apparatus for removing unwanted fluids from fluid mixtureswere not available. Although specific problems are described in thisbackground section, the invention is not limited to solving theseparticular problems. Embodiments of the present invention may be usefulin solving other problems not specifically described in this section.Thus, the background section should not be used to limit the scope ofthe appended claims.

SUMMARY OF THE INVENTION

One embodiment of the invention provides a system and apparatus thatefficiently and cost effectively removes a fluid from a fluid mixture,such as methane from water containing methane, radon from ground wateror liquid hydrocarbons from water.

In one embodiment, a fluid mixture having a first fluid component and asecond fluid component is introduced into a process stream. The localvelocity of the fluid mixture is changed by passing the mixture througha plurality of restrictions. The change in local velocity causes atleast a portion of the first fluid component to separate from the fluidmixture. At least a portion of the first fluid component separated fromthe fluid mixture is discharged along with at least a portion of thesecond fluid component. In certain embodiments, the first fluidcomponent is collected. In other embodiments, the first fluid componentis collected under negative pressure. In some embodiments, thetemperature of the fluid mixture is changed. In other embodiments,baffles are used to change the rate of flow of the fluid mixture. Thebaffles may be generally horizontal, and in some embodiments, conical.

In one embodiment, the fluid mixture is passed through a chamber aftercausing the mixture to repeatedly change velocity. In one aspect of theinvention, the fluid mixture enters the chamber through a firstplurality of apertures. In another embodiment, the fluid mixture exitsthe chamber through a second plurality of apertures. In yet anotherembodiment, the fluid mixture is caused to rotate around the mixture'sgeneral axis of flow through the chamber by impinging upon a surfaceangled relative to the mixture's general axis of flow. In oneembodiment, the fluid mixture is caused to rotate around the mixture'saxis of flow through the chamber by introducing the mixture into thechamber through nozzles angled relative to the fluid mixture's generalaxis of flow.

In one embodiment, the process is used to process a mixture of water andmethane.

In another embodiment, the restrictions through which the fluid passesare a plurality of apertures within a conduit, the apertures having across-sectional area smaller than the average cross-sectional area ofsaid conduit. The fluid mixture is then passed through a chambercontaining a baffle, the baffle facilitating the aggregation of gasbubbles in the fluid mixture.

In one embodiment, the mixed fluid includes a first fluid component anda second fluid component. The mixed fluid is cause to experienceturbulent flow within a conduit. The turbulent flow causes a portion ofthe first and second fluid components to separate. The mixed fluid iscaused to experience laminar flow within the conduit. The laminar flowfacilitates further separation of the first and second fluid components.At least a portion of the separated first fluid component is removedfrom the conduit. At least a portion of the second separated fluidcomponent is also removed from the conduit. In another embodiment, theturbulent flow is caused by passing the mixed fluid through arestriction. In yet another embodiment, the mixed fluid experiencescentrifugal force. In one embodiment, the first fluid component ismethane and said second fluid component is water.

Another embodiment of the invention comprises a fluid separation system.The system has a first chamber causing a mixed fluid comprising a firstfluid component and a second fluid component to experience turbulentflow when passed through the first chamber. A second chamber causes themixed fluid to experience laminar flow when passed through the secondchamber. The turbulent flow and laminar flow causes a portion of thefirst fluid component to aggregate. A first fluid component removalorifice is in fluid communication with the aggregated first fluidcomponent. A second fluid component removal orifice is in fluidcommunication with the second fluid component. In one embodiment, thesecond chamber contains a plurality of baffles. In another embodiment,the baffles are conical.

In yet another embodiment, a third chamber facilitates gravityseparation of the first fluid component from the second fluid component.The third chamber has the first fluid component removal orificepositioned in fluid communication with the gravity separated first fluidcomponent. The third chamber also has the second fluid component removalorifice positioned in fluid communication with the gravity separatedsecond fluid component. In some embodiments, the mixed fluid contains athird fluid component. The third chamber facilitates gravity separationof the third fluid component from the first fluid component and thesecond fluid component. The third chamber has a third fluid componentremoval orifice positioned in fluid communication with the gravityseparated third fluid component.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a partial cut away perspective view of one embodiment of afluid separation system.

FIG. 2 is a front view of one embodiment of an agitation chamber inletplate.

FIG. 3 is a front view of a second embodiment of an agitation chamberinlet plate.

FIG. 4 is a front view of one embodiment of an agitation chamber outletplate.

FIG. 5 is a top view of one embodiment of a first baffle.

FIG. 6 is a top view of one embodiment of a second baffle.

FIG. 7 is a cut away side view of one embodiment of a separationchamber.

FIG. 8 is a partial cut away perspective view of one embodiment of afluid separation system.

FIG. 9 is a top view of one embodiment of an agitation chamber inletplate with the top portion joining sub-plates removed.

FIG. 10 is a top view of one embodiment of an agitation chamber outletplate with the top portion joining sub-plates removed.

FIG. 11 is a cut away top view of one embodiment of a collectionchamber.

FIG. 12 is a partial cut away side view of one embodiment of a fluidseparation system.

FIG. 13 is a plan view of one embodiment of a separation system havingmultiple separation chambers and agitation chambers.

DETAILED DESCRIPTION OF THE INVENTION

This disclosure is intended to describe the novel features of theclaimed invention. Those of ordinary skill in the art will recognizealternate equivalent methods and devices for removing fluids from fluidmixtures upon reading this disclosure.

FIG. 1 depicts a cut away perspective view of an embodiment of the fluidseparation system 7 that is adapted for removal of a fluid from a fluidmixture, such as methane from water. The methane-laden water may bewater pumped from a coal seam or from an aquifer.

While it is currently contemplated that the invention will be used withgroundwater, i.e., water found below the earth's surface, the inventionsgeneral application is not so limited. For example, it is contemplatedthat the invention can be used to separate liquid hydrocarbons fromwater at the earth's surface, such as water contaminated with crude oilor petroleum derived products. Also, the invention is not limited to theseparation of hydrocarbons from water as it can be used to separateradon from water as well. Additionally, as presently contemplated, theinvention is not limited to separation of fluids from water. Forexample, it is contemplated that the invention can be used to separategaseous hydrocarbons from liquid hydrocarbons.

After being removed from a coal seam or aquifer and being pumped to theearth's surface, water containing methane is introduced into the systemat inlet 9. An inlet valve 10 is placed in the flow path and may be usedto control the rate of flow of the fluid mixture into conduit 11. Inletvalve 10 is a typical ball valve as will be known to one of ordinaryskill. A check valve 12 prevents back-flow. A strainer 14, such asmanufactured by Mueller Manufacturing, having approximately 20 openingsper square inch, removes solid particulates that may be in the fluid. Aflow meter 16 monitors the rate of fluid flow and can provide data used,in conjunction with inlet valve 10, to control the rate of fluid flowthrough the fluid separation system 7. With the embodiment described,the desired rate of flow is typically between approximately 7 and 10gpm. The fluid mixture passes through screen 17 having approximately10-20 openings per square inch.

As the fluid mixture passes through strainer 14 and screen 17, thevelocity of the fluid changes. Herein, velocity includes direction offlow and speed (the time rate of change of the position of discretefluid components without regard to direction). The fluid's speedincreases as it passes through strainer 14 and screen 17 because thecross-sectional area of the flow path is decreased and the speed of thefluid passing through the decreased area must increase to maintain theoverall rate of fluid flow through the fluid separation system 7. Thevelocity of the fluid also changes because the fluid must changedirection to pass through the openings in strainer 14 and screen 17.

After flowing through screen 17, the fluid is introduced into anagitation chamber 18 that has a diameter approximately four to 9 timeslarger than the conduit 11 and is 2-3 times its diameter in length.Specifically, in the embodiment described, the conduit 11 has an insidediameter of approximately one inch and the agitation chamber 18 has aninside diameter of approximately eight inches.

At the proximal end of the agitation chamber 18 is an agitation chamberinlet plate 19. In one embodiment, as shown in FIG. 2, agitation chamberinlet plate 19 has three inlet orifices 24 formed in nozzles 26 that areangled relative to the longitudinal axis of agitation chamber 18. In theembodiment depicted, the inlet orifices 24 have an inside diameter ofapproximately ⅜ inch.

In the embodiment depicted in FIG. 2, the fluid exits the inlet orifices24 at an angle relative to the longitudinal axis of agitation chamber 18and impinges on the inner wall of the agitation chamber 18. It ispresently contemplated that nozzles 26 would be angled such that theresulting fluid flow tends to rotate around the longitudinal axis of theagitation chamber 18 as it progresses through the agitation chamber 18.All of the nozzles can be angled approximately 30 degrees from the Zaxis of FIG. 2 and, as depicted, approximately 60 degrees down from theX axis for the upper right nozzle, approximately 60 degrees left of theY axis of FIG. 2 for the lower nozzle and approximately parallel withthe Y axis of FIG. 2 for the left nozzle.

In this embodiment, the velocity of the fluid changes because thedirection of fluid flow changes from being generally parallel to thelongitudinal axis of the agitation chamber 18 prior to entering nozzles26 to being angled relative to the same axis. Also, the fluid's speedchanges from a lower rate prior to entering the nozzles 26 to a higherrate as it accelerates and passes through the nozzles 26. As the fluidexits the inlet orifices 24, its speed decreases and, as the fluidimpinges on the agitation chamber 18 inner wall, the direction of flowbecomes rotational and velocity constantly changes with the rotationalflow. Thus, both aspects of velocity, e.g., speed and direction of flow,are changed as the fluid enters the agitation chamber 18. Additionally,the rotational flow imparts a centrifugal force on the fluid.

FIG. 3 depicts an alternate embodiment of the agitation chamber inletplate 19. In this embodiment, the agitation chamber inlet plate 19 hasthree inlet orifices 24. The inlet orifices 24 have an inside diameterof approximately ⅜ inch. The inlet orifices 24 are formed into theagitation chamber inlet plate 19 and paths through the inlet plate 19are generally parallel to the longitudinal axis of the agitation chamber18. An impeller 28 is adjacent the inlet orifices 24. The impeller 28has a diameter of approximately 7½ inches. As the fluid enters theagitation chamber 18 through inlet orifices 24, it impinges on impeller28 and causes impeller 28 to rotate. Impact with impeller 28 causes thefluid to deflect at an angle relative to the longitudinal axis of theagitation chamber 18.

Many alternative structures could be used to change the velocity of thefluid in the agitation chamber 18. For example, impeller 28 could bereplaced with fixed vanes. Also, rather than imparting a rotationalflow, the velocity of the fluid could be changed by repeatedly forcingthe fluid in one linear direction and then another.

FIG. 4 depicts the agitation chamber outlet plate 30 that is located atthe distal end of the agitation chamber 18. In this embodiment, theagitation chamber outlet plate 30 has six outlet plate orifices 32. Theoutlet plate orifices 32 change the velocity of the fluid. The outletplate orifices have a diameter of approximately ½ inch. The outlet plateorifices 32 are formed in the outlet plate 30 and the fluid flow paththrough the outlet plate 30 is generally parallel to the longitudinalaxis of the agitation chamber 18. In this embodiment, the agitationchamber outlet plate 30 is approximately 18 inches from the agitationchamber inlet plate 19. FIG. 4 merely shows one embodiment of an outletplate 30. In other embodiments, outlet plate 30 may be designed withdifferent orifices or other features.

After the fluid passes through the outlet plate 30, it passes through areducer to separation chamber inlet piping 34 and enters the bottom ofthe separation chamber 36. The inlet piping 34 has an inside diameter ofapproximately 4 inches.

The separation chamber 36 provides conditions conductive to thecollection or aggregation of the fluid to be collected. The separationchamber 36 changes the velocity of the fluid mixture. In general, thespeed of the fluid mixture is greatly reduced as it passes through theseparation chamber 36 and the flow is relatively calm because therestrictions on the fluids flow are reduced. When methane is processed,the separation chamber 36 encourages bubbles of methane to join and formlarger bubbles. When the fluid to be collected is a liquid, theseparation chamber 36 encourages droplets of the liquid to be collectedto join and form larger droplets.

In the embodiment shown in FIG. 1, the separation chamber 36 isgenerally cylindrical and has a diameter of approximately 24 inches thatis defined by sidewall 38. The separation chamber 36 is approximately 36inches tall. The fluid entering the separation chamber 36 next passesthrough arcuate slots 40 defined between the separation chamber sidewall38 and a first baffle 42, as shown in FIG. 5. The first baffle 42 isconical in shape. In one embodiment, the arcuate slots 40 areapproximately 23 and ⅔ inches long adjacent the separation chambersidewall 38 and are approximately one inch wide. The apex of the firstbaffle 42 is approximately ⅛th the separation chamber 36 diameter belowthe arcuate slots 40.

The separation chamber 36 has a second baffle 44 above the first baffle42 that is also conical in shape and has aperture 46 in place of theapex of the cone. The base of second baffle 44 is connected to sidewall38. The apex of the second baffle 44 is approximately ⅛th the separationchamber 36 diameter above the base of the second baffle 44. The aperture46, as shown in FIG. 6, in the second baffle 44 has a diameter of 4inches.

A third baffle 48 is above the second baffle 44. The third baffle 48defines arcuate slots 50 between the separation chamber sidewall 38 andthe third baffle 48 periphery. The third baffle 48 is identical to thefirst baffle 42 and has its apex below slots 50. The base of thirdbaffle 48 is approximately ⅛th of the diameter of the separation chamber36 above the apex of the third baffle 48.

The second baffle 44 apex is approximately midway between the top andbottom of the separation chamber 36. The base of the first baffle 42 isapproximately midway between the apex of the second baffle 44 and thebottom of the separation chamber 36. The base of the third baffle 48 isapproximately midway between the apex of the second baffle 44 and thetop of the separation chamber 36.

FIG. 7 is a cross-sectional view of the separation chamber 36. Asdepicted in FIG. 7, the first conical baffle 42 has arcuate slots 40between the first baffle 42 and the separation chamber sidewall 38. Thesecond conical baffle 44 has an aperture 46 at its apex and is connectedto the sidewall 38 at its base. The third baffle 48 is depicted with itsapex below arcuate slots 50.

The fluid exits the separation chamber 36 through collection chamberinlet piping 52 that has an inside diameter of one inch. The collectionchamber inlet piping 52 connects to an inlet piping expander 54 thatincreases the diameter of the fluid flow path to approximately fourinches. The fluid passes through inlet piping and inlet piping expander54 to collection chamber 56. Collection chamber 56 has a diameter ofapproximately four inches and is approximately 48 long.

Because methane separated by the process from the coal seam water islighter than water, it tends to rise in the collection chamber 56 whilethe water falls in the collection chamber 56. In one embodiment, a sighttube is connected to the collection chamber 56 so the surface elevationof the water can be monitored. It is generally desired that the waterfill the bottom ⅔ to ¾ of the collection chamber 56. One of ordinaryskill in the art would recognize that known sensors could replace thesight tube and could be configured to automatically regulate inlet fluidflow to maintain the proper water level in collection chamber 56.

Water is discharged from discharge outlet 58 at the bottom of collectionchamber 56. The discharge outlet 58 has a diameter of approximately twoinches.

Methane is collected through collection outlet 60. Collection outlet 60has a diameter of approximately one inch. In some applications, it maybe desirable to create a partial vacuum at collection outlet 60. Thecollected methane may be used as a fuel source, as is commonlyunderstood.

The fluid separation system 7 is sealed when used to collect methane, orother gases. In other words, the fluid mixture is not exposed to theatmosphere as it passes through the fluid separation system 7 andseparated gases cannot leave the fluid separation system 7 exceptthrough the collection outlet 60. If small amounts of gas remain in thefluid mixture at the end of the process, this unseparated gas can onlyleave the fluid separation system with the processed fluid mixturethrough discharge outlet 58.

In some embodiments, it may be advantageous to modify the temperature ofthe fluid as it is processed. FIG. 8 depicts a system adapted to modifyfluid temperature. In one embodiment, the agitation chamber 118 has atemperature modifying agitation chamber inlet plate 119 at its proximalend. The temperature modifying agitation chamber inlet plate 119 isformed by creating a void 121 between adjacent sub-plates 123, asdepicted in FIG. 9. FIG. 9 is a top view of the temperature modifyingagitation chamber inlet plate 119 with the member joining the sub-plates123 removed. Tubes 125 provide a fluid flow path through the temperaturemodifying agitation chamber inlet plate 119. A void 121 is defined bythe adjacent surfaces of the sub-plates 123, the exterior walls of tubes125 and the interior wall of the surface joining the adjacent sub-platesat their periphery. Inlet port 127 and outlet port 129 provide a flowpath for heating or cooling fluids through the void 121.

Temperature modifying agitation chamber outlet plate 130 may besimilarly constructed with inlet port 131 and outlet port 132 providinga flow path for heating or cooling fluid between the outlet sub-plates133 and around outlet tubes 134, as depicted in FIG. 10. FIG. 10 is atop view of the temperature modifying agitation chamber outlet plate 130with the member joining the sub-plates 133 removed.

Additionally, an optional lower tubing coil 135 may be placed betweenthe bottom of the separation chamber 136 and the first baffle 142. Thelower tubing coil 135 is depicted in FIG. 11. The coil may be made of⅜th inch copper tubing that is spaced such that there is approximately a⅜th inch gap between adjacent tubing outer walls. The lower tubing coil135 has an inlet port 143 through the sidewall 138 and an outlet port145 through the sidewall 138 that provides a flow path for heating orcooling fluids to pass through the lower tubing coil 135. An optionalupper tubing coil 170 may be placed between the second baffle 144 andthe third baffle 148 as depicted in FIG. 8. The upper tubing coil 147has an inlet slot 151 and an outlet 153 to provide a flow path forheating or cooling fluids to pass through the upper tubing coil 147.

In embodiments, heating or cooling may be desirable depending upon thenature of the fluid processed. Heating fluids having relatively highviscosity may enhance separation. Conversely, some processed fluids mayhave a high native temperature detrimental to fluid separation. Coolingsuch fluids may enhance separation. In some applications, it may bedesirable to heat fluid at one stage of the process and to cool thefluid at another stage of the process. It is contemplated that thechange in processed fluid temperature will be greater than five degreesFahrenheit. Described above are methods of modifying the temperature ofthe processed fluids. The description is not exhaustive and one ofordinary skill will be aware of equivalent methods of modifying thetemperature of a fluid being processed.

FIGS. 12 and 13 depicts an embodiment of a separation system designed toseparate fluids such as might be encountered at a crude oil spill or awaste oil stream. FIG. 12 depicts the system laid out in a linearfashion. FIG. 13 is a top view of the system as it might be constructedto maximize space utilization. An optional agitation chamber 218 with anagitation chamber inlet plate 219 and an agitation chamber outlet plate230 may be provided if it enhances fluid separation. It may bedesirable, for example, to pass a fluid through the agitation chamber218 if the fluid contains a gas component. If fluid separation isenhanced by use of the optional agitation chamber 218, it flows from theagitation chamber 218 through the fluid separation chamber inlet piping234 into the separation chamber 236. If the agitation chamber 218 is notused, the fluid to be processed may be introduced directly into theseparation chamber inlet piping 234.

FIG. 12 depicts a cross-section view of the separation chamber 236.Separation chamber 236 is generally as described above and has anoptional lower tubing coil 235 that may be used if fluid temperaturemodification is desired. The lower tubing coil 235 is placed between thefirst baffle 242 and the bottom of the separation chamber 236 and has aninlet port 237 through the sidewall 238 and an outlet port 239 that alsopasses through the sidewall 238. Above the second baffle 244 is optionalupper tubing coil 247 and the third baffle 248. The upper tubing coilhas an inlet 251 and an outlet 253.

The fluid exists the separation chamber 236 through collection chamberinlet piping 252. A valve 255 is placed in the collection chamber inletpiping 252 to permit isolation of an individual separation chamber 236from the collection chamber 256. FIG. 12 depicts a single agitationchamber 218 and separation chamber 236 feeding a common collectionchamber 256. The collection chamber 256 in FIG. 12 is depicted incross-section. In the embodiments depicted in FIGS. 12 and 13, it iscontemplated that four separation chambers 236 will feed the commoncollection chamber 256.

If a gas is separated from the processed fluid, it is collected throughoutlet 260. If fluids having different specific gravities are separated,such as oil and water, the fluid with the lower specific gravitycollects in the upper portion of collection chamber 256 and can becollected through outflow line 262 to a storage container 264. When adesired quantity is collected, valve 266 may be opened and the collectedfluid removed. It may be advantageous to heat outflow line 262 and/orstorage container 264 if the collected fluid is viscous. It iscontemplated that in some embodiments the system can separate gas andliquids having different specific gravities from the same fluid mixture.

The fluid with the greater specific gravity naturally collects at thelower portion of collection chamber 256. A siphon tube 267 draws thefluid from the lower portion of the collection chamber 256 anddischarges it through outflow pipe 268. The siphon tube 267 has asuction release aperture 269 positioned to break the suction drawing thefluid from the collection chamber 256 if the fluid level in thecollection chamber reaches the suction release aperture 269. Suchprevents the fluid with the lower specific gravity from being drawn intothe siphon tube 267.

It is also contemplated that in some embodiments conventional sensorswill be used to regulate the flow of processed fluid into the separationsystem such that the level of the fluid with the higher specific gravityremains above siphon tube 267 and below outflow line 262.

It is contemplated that embodiments of the inventions disclosed hereinmay be used in series or in parallel depending on the nature and volumeof the fluid being processed and the nature and number of fluids beingseparated from the processed fluid. FIGS. 12 and 13 depict an embodimentadapted to process a larger quantity of fluid and separating threefluids from the processed fluid, specifically, a gas and two liquidshaving different specific gravities, more specifically, gaseoushydrocarbons, oil and water.

As depicted in FIG. 13, a main inlet line 270 supplies the fluid beingprocessed to a pair of inlet valves 272. As noted above, inlet valves272 may be controlled to manage the fluid levels in the collectionchamber 256 based upon output from conventional sensors in thecollection chamber 256. Check valves 274 are adjacent to the inletvalves 272. The system depicted has a pair of optional agitationchambers 218, as described above. Each agitation chamber 218 suppliesfluid to two separation chambers 236, as previously described. Eachseparation chamber 236 is connected to the collection chamber 256 bycollection chamber inlet piping 252.

In the embodiment described, for a flow rate of 250 gpm, it iscontemplated that the separation inlet piping 234 has a diameter of 8inches. The separation chambers 236 have a 60 inch inside diameter. Thebase of the first baffle 242 is 2 feet, 1 and 13/16th inches from thebottom of the separation chambers 236. The base of the second baffle 244is one foot, 3 13/16 inches from the base of the first baffle 242. Theapex of the third baffle 248 is one foot 7 5/16 inches from the base ofthe second baffle 244. Each baffle 242, 244, 248 tapers approximately1.5 to 2 degrees from horizontal as it progresses from base to apex. Theseparation chambers 236 are eight feet 5 inches tall.

The base of the collection chamber 256 has an outside diameter of 48inches and the inlet of the siphon tube 266 is one foot 6 inches abovethe bottom of the collection chamber 256. The collection chamber 256 is13 feet, 6 and 11/16th inches tall. The bottom of the outflow line 262is 15 inches below the top of the collection chamber 256. The bottom ofthe collection chamber inlet piping is nine feet 11/16 inches above thebottom of the collection chamber 256.

One skilled in the art will recognize that the principals of the claimedinvention can be practiced in a number of different ways. By way ofexample, one of ordinary skill will recognize that the number, placementand shape of the baffles and heating elements may by modified to achievethe desired result. Moreover, the configuration of the baffles and thedescribed inlet and outlet plates could be modified and achieve the samepurpose. For example, the conical baffles described could be replaced byplanar baffles positioned at an angle with apertures at the downstreamside of the angled baffle and the downstream side of the angle bafflebeing upward of the lower portion of the baffle. Similarly, the inletand outlet plates could be replaced by a series of baffles causingrepeated velocity charges.

One skilled in the art will recognize that components may be eliminatedwithout significantly affecting the functionality of the disclosedsystems. For example, the strainer and screen could be eliminated andthe system would perform substantially the same way.

The invention can be scaled for larger or smaller flows. The agitationchamber and/or separation chamber can be arraigned in parallel orseries, or used in the opposite order, depending on the conditions ofthe fluid mixture to be processed and the requirements of the specificlocation. In some settings the agitation chamber may be undesirable.

After reviewing the disclosure of the claimed invention, numerousmodifications would be apparent to one of ordinary skill in the art toachieve the same result as the claimed invention.

1-25. (canceled)
 26. A method for removing a gas from a fluid, themethod comprising: introducing the fluid into a first chamber; changinga velocity of the fluid by passing the fluid through a plurality ofrestrictions; and collecting, at a collection outlet, at least a portionof the gas that is separated from the fluid as a result of the changingvelocity.
 27. The method of claim 26, further comprising discharging atleast a portion of the fluid.
 28. The method of claim 26, wherein thegas is a volatile gas and wherein the fluid is at least one of: (i)groundwater, (ii) water, (iii) oil, and (iv) a combination thereof. 29.The method of claim 26, wherein the at least the portion of the gas thatis collected at the collection outlet is used as a fuel source.
 30. Themethod of claim 26, wherein the temperature of the fluid is changed morethan five degrees Fahrenheit.
 31. The method of claim 26, whereinvelocity of the fluid is changed using one or more baffles.
 32. Themethod of claim 31, wherein the baffles are generally horizontal. 33.The process of claim 31, wherein the baffles are conical.
 34. A methodfor separating one or more fluid components from a fluid, the apparatuscomprising: introducing the fluid into a contained flow path; separatingat least a first fluid component of the one or more fluid componentsfrom the fluid using one or more different flows; and collecting, forsubsequent use, at least a portion of the at least the first fluidcomponent that was separated from the fluid.
 35. The method of claim 34,wherein the subsequent use is use as a fuel source.
 36. The method ofclaim 34, wherein the at least one of the one or more different flows isa laminar flow.
 37. The method of claim 34, wherein at least one of theone or more different flows is a turbulent flow and wherein theturbulent flow is caused by passing the fluid through a restriction inthe contained flow path.
 38. The method of claim 34, wherein the fluidis at least one of: (i) water and (ii) oil, and wherein the at least thefirst fluid component is a volatile gas.
 39. The method of claim 38,wherein the volatile gas is methane.
 40. An apparatus for separating oneor more volatile gasses from a fluid, the apparatus comprising: avelocity changing area configured to cause the fluid to experience aplurality of velocities; a flow area configured to cause the fluid toexperience one or more types of flow, wherein the one or more types offlow cause at least a portion of the one or more volatile gasses in thefluid to aggregate; and a removal orifice configured to collect andstore the aggregated one or more volatile gasses.
 41. The apparatus ofclaim 40, wherein flow area contains a plurality of baffles.
 42. Theapparatus of claim 41, wherein the baffles are conical.
 43. Theapparatus of claim 40, further comprising a chamber for facilitatinggravity separation of the one or more volatile gasses from the fluid.44. The apparatus of claim 43, wherein the chamber comprises a firstremoval orifice positioned in fluid communication with the one or morevolatile gasses separated by the gravity separation.
 45. The apparatusof claim 40, further comprising a flow path, wherein the flow path iscoupled to the velocity changing area and further wherein the flow pathis coupled to a pumping component.